US4586942A - Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas - Google Patents

Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas Download PDF

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US4586942A
US4586942A US06/575,541 US57554184A US4586942A US 4586942 A US4586942 A US 4586942A US 57554184 A US57554184 A US 57554184A US 4586942 A US4586942 A US 4586942A
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ambient temperature
cooling
mixture
liquid
fluid
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Pierre Gauthier
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0267—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using flash gas as heat sink
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/284—Special features relating to the compressed vapour
    • B01D1/2856—The compressed vapour is used for heating a reboiler or a heat exchanger outside an evaporator
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/2884—Multiple effect compression
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

Definitions

  • the present invention relates to a process and a plant for cooling a fluid which apply in particular to the liquefaction of natural gas. It concerns first of all a cooling process of the type in which a cooling mixture composed of constituents having different volatilities is compressed in at least two stages and in which, after the last compression stage and after at least one intermediate compression stage, the mixture is partly condensed, and the condensed fractions are expanded and vaporized in heat exchange with the fluid to be cooled before being compressed again.
  • the condensation of a slightly volatile fraction effected after said intermediate stage has for purpose to provide an increased cooling effect in the warm part of the heat exchange line at the cost of a low specific energy owing to the reduced rate of compression of this fraction.
  • This slightly volatile fraction permits the reduction in this region of the temperature difference between the cooling mixture and the fluid or fluids to be cooled, which difference corresponds to a thermodynamic irreversibility.
  • the resulting gain is marked only if the mixture thus condensed at medium pressure has a sufficiently high bubble temperature and/or if its flow rate is sufficiently high.
  • the cooling mixture is usually constituted by a mixture of C 1 to C 5 hydrocarbons with, if desired, a small proportion of nitrogen, so as to be able to produce a cooling effect at optimum temperature levels, it is necessary to render the mixture heavier in order to achieve a marked saving of energy.
  • An object of the invention is to reduce the compression energy without the use of constituents which are liable to become solidified in the cold part of the exchange line.
  • the invention therefore provides a cooling process of the afore-mentioned type, wherein at least one of the condensation stages is carried out by sending into a distillation column the mixture issuing from the corresponding stage of the compressor.
  • the distillation is effected solely after the last compression stage, and the condensate resulting from this distillation, and the other condensate or condensates, are sub-cooled to the same temperature and, after expansion, united in the same pipe before being put into heat exchange relation with the fluid to be cooled.
  • a distillation is carried out at an intermediate compression stage of the condensate resulting from the distillation is sub-cooled to a first temperature and the condensate of the following compression stage or stages are sub-cooled to a second temperature lower than the first temperature.
  • Another object of the invention is to provide a plant for carrying out such a process.
  • This plant is of the type comprising a refrigeration circuit in which is circulated a cooling mixture and which includes a compressor having at least two stages each provided with a cooler, and a liquid-vapour separator following on the cooler of the last stage and following on that of at least an intermediate stage relative to the flow in said circuit, wherein there is interposed between the cooler associated with at least one of the separators and the corresponding compressor stage a distillationn column which is heated by the gas compressed by said compressor stage in which is refluxed the liquid issuing from the separator.
  • FIG. 1 is a diagram of a natural gas liquefaction plant according to the invention.
  • FIG. 2 is a diagram illustrating the advantage afforded by such a plant.
  • FIGS. 3 and 4 are partial diagrams of two other embodiments of the plant according to the invention.
  • the plant shown in FIG. 1 is adapted to cool, liquefy and sub-cool natural gas flowng in a pipe 1 at ambient temperature at a pressure of the order of 40 or 50 bars.
  • This plant employs for this purpose a cooling cycle of the so-called incorporated cascade type. This cycle is closed in that the cooling mixture circulates in pipes completely separated from the pipe 1.
  • the cooling mixture is a mixture of C 1 to C 5 hydrocarbons, for example methane, ethane, propane, butane and pentane, and nitrogen. It is compressed in two stages: it is drawn in at low pressure (of the order of 3 bars) by a first compressor stage 2 which discharges it at medium pressure (of the order of 12 bars) into a pipe 3. The mixture passes through an intermediate cooler 4 supplied with sea water where it is partly condensed. The two phases are separated in a separator 5 and the resulting vapour is compressed at high pressure (of the order of 50 bars) by a second compressor stage 6.
  • C 1 to C 5 hydrocarbons for example methane, ethane, propane, butane and pentane, and nitrogen. It is compressed in two stages: it is drawn in at low pressure (of the order of 3 bars) by a first compressor stage 2 which discharges it at medium pressure (of the order of 12 bars) into a pipe 3.
  • the mixture passes through an intermediate cooler 4 supplied with sea water where it is partly condensed.
  • the gas issuing from the latter at about 140° C. is directly sent to the lower portions or tank of a distillation column 7 having a very small number of theoretical plates, for example two theoretical plates.
  • the head vapour is cooled and partly condensed in a cooler 8 which also employs sea water and the condensate, which is received in a separator 9, is refluxed in the column 7.
  • a first liquid L1 at medium pressure, which is the liquid received in the separator 5; a second liquid L2, at high pressure, which is the tank liquid of the column 7; and the gas G issuing from the final separator 9.
  • the liquid L1 and the gas G are at subsequently the same temperature, of the order of 40° C., imposed by the use of sea-water in the coolers 4 and 8.
  • the liquid L2 is brought back to substantially the same temperature by passage through a sea-water cooler 10.
  • the three fluids L1, L2 and G pass travel in co-current manner with the natural gas through a first heat exchanger 11 which constitutes the "warm" part of the heat exchange line.
  • a first heat exchanger 11 which constitutes the "warm" part of the heat exchange line.
  • these two liquids are expanded to low pressure in respective relief-valves 12 and 13 and then united in a pipe 14 and vaporized in counter-current manner with respect to the natural gas in the exchanger 11, the vapour being super-heated in the warm part of this exchanger and then brought back to the intake side of the compressor stage 2 at roughly ambient temperature.
  • the gas G After having passed through the exchanger 11 where it is partly condensed, the gas G passes through a second heat exchanger 15 where it is completely liquefied and sub-cooled; at the cold end of the exchanger 15, that is at the final temperature desired for the natural gas liquefied at high pressure (-150° C. to -161° C.), this liquid, which is sufficiently sub-cooled, is expanded to low pressure in a relief-valve 16 and sent through a pipe 17 to be vaporized in the exchanger 15 in a counter-current manner with respect to the natural gas. The vapour is then united with the liquids L1 and L2 flowing in the pipe 14 so that these three fluids together form a diphase fluid which vaporizes and provides the required cooling effect in the exchanger 11.
  • the plant may be completed as shown by the following arrangements.
  • the natural gas is brought out of this exchanger and sent to a gasoline-extracting unit (not shown) where certain heavy products are extracted.
  • the remaining products for example at two different pressures, are reintroduced at 19A and 19B in the exchanger 15 so as to complete their cooling, their liquefaction and their sub-cooler.
  • the two sub-cooled fractions of the natural gas are expanded as they leave the exchanger 15 in one or more steps to a pressure in the neighbourhood of atmospheric pressure in respective relief-valves 20 and 21 and then united in a pipe 22 so as to be sent to a storage tank 23.
  • the vapour formed in this tank which brings the liquefied natural gas to its equilibrium temperatures of about -161° C., is discharged through a pipe 24, passes through a heat exchanger 25 where it is heated and is recompressed by a compressor 26 for sending through a pipe 27 to the "fuel gas" utilization network.
  • a branch pipe 28, connected to the pipe 1 upstream of the exchanger 11 and equipped with a relief-valve 29, enables an additional supply of gaseous natural gas to be sent to the pipe 27 if necessary.
  • a pipe 30 is connected to the pipe of the gas G between the separator 9 and the exchanger 11 and passes through the exchanger 25, in which the gas G is liquefied and sub-cooled. This liquid is expanded to low pressure in a relief-valve 31 and then mixed with the low-pressure fluid issuing from the relief-valve 16.
  • the cooling effect of the boil-off of the storage may serve to cool and liquefy a fraction of the initial natural gas.
  • the flow rate and the composition of the high-pressure vapour are predetermined so as to ensure the cooling balance in the exchanger 15.
  • the foregoing reasoning shows that the invention gives the same composition of high-pressure vapour with a mixture that is heavier than in the prior art. This heavier mixture will produce a higher flow rate of liquid L1 in the separator 5 for given pressure and temperature.
  • the sum of the flow rates of the liquids L1 and L2 is also predetermined, as a first approximation, for ensuring the cooling balance in the exchanger 11.
  • the fluid L1+L2 is rendered heavier; as it concerns a mixture of hydrocarbons, its vaporization heat is increased. Consequently, a lower overall flow is sufficient to ensure the cooling balance in the exchanger 11, which also contributes to a reduction in the compression energy.
  • the high-pressure circuit requires no interruption since the fluid G flowing therein contains no components liable to be solidified therein. In practice, such components could be tolerated as impurities in the cycle mixture, in a proportion which is low enough to avoid exceeding their solubility limit in the other constituents of the mixture of the employed range of temperatures. Further, the sole interruptions required in the medium-pressure and low-pressure circuits consist in withdrawing the liquids L1 and L2 at medium pressure and simultaneously reinjecting them at low pressure. Consequently, although the exchange line has been shown to include two distinct exchangers 11 and 15, it is quite possible to provide a single heat exchanger covering the whole range of temperatures of the treatment of the natural gas.
  • This plant may again be compared with a plant of the prior art devoid of a distillation column, i.e. in which the pipe 3 leads directly to the cooler 4B and in which the liquid received in the separator 5 is directly sent to the exchanger 11; for given flow rate and composition of the high-pressure gas G, the liquid L3 contained in the separator 9 has a given composition.
  • the intermediate pressure between the two compression stages defines the flow rate of the liquid L3 which permits obtaining a mixture whose dew point is the temperature of the separator 5.
  • the flow rate and composition of the vapour issuing from the separator 5 are consequently unchanged.
  • the liquid L1 In the absence of the column 7, the liquid L1 is in equilibrium with said vapour; with the column 7, as the liquid L1 is heavier, it has an increased vaporization heat, so that a lower flow rate is sufficient to ensure the cooling balance of the exchanger 11.
  • the liquid L1 is very heavy, it is desirable to sub-cool it to an intermediate point of the exchanger 11, as shown in FIG. 3, before expanding it to low pressure in a relief-valve 12A and then reinjecting it into the exchanger 11 at the same temperature, for example -10° C., for its vaporization, mixed with the already expanded two high-pressure fluids L3 and G. In proceeding in this manner, the liquid L1 does not hinder the vaporization of the lighter liquid L3.
  • the flow rate compressed by the first stage 2 is reduced and the cooling effect of the liquid L1 occurs at a higher temperature level, precisely in the excessive temperature difference zone seen in FIG. 2.
  • the introduction of the column 7 reduced the irreversibility, on the one hand, at the warm source 4B for the same reason as in the case of FIG. 1 and, on the other hand, by the reduction of the temperature difference in the warm part of the exchange line.
  • the discharge pipe 3 of the first stage 2 leads directly to the tank of a first distillation column 7A.
  • the tank liquid L1 passes into a sea-water cooler 4A and is sub-cooled in the warm part of the exchanger 11.
  • the head vapour passes into a sea-water cooler 4B and then reaches a separator 5.
  • the liquid received in the latter is refluxed in the column 7A while the vapour is supplied to the second compressor stage 6.
  • the gas issuing from the latter is directly supplied to the tank of a second distillation column 7B.
  • the tank liquid L2 passes into a sea-water cooler 10 and is sub-cooled in passing through the whole of the exchanger 11.
  • the head vapour passes into a sea-water cooler 8 and then reaches a separator 9.
  • the liquid L3 received in the latter is refluxed in the column 7B while the vapour G constitutes the high-pressure cooling fluid.
  • each distillation column 7, 7A, 7B is heated by the direct injection into the column of the compressed gas issuing from the corresponding compressor stage 2 or 6.
  • this compressed gas could pass through a heat exchanger coil disposed in the tank of the column and heating the latter, before being injected into the column at a suitable height.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US06/575,541 1983-02-08 1984-01-31 Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas Expired - Lifetime US4586942A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8301919A FR2540612A1 (fr) 1983-02-08 1983-02-08 Procede et installation de refroidissement d'un fluide, notamment de liquefaction de gaz naturel
FR8301919 1983-02-08

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US4586942A true US4586942A (en) 1986-05-06

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US (1) US4586942A (de)
EP (1) EP0117793B1 (de)
AR (1) AR231586A1 (de)
AT (1) ATE15938T1 (de)
BR (1) BR8400537A (de)
CA (1) CA1227124A (de)
DE (1) DE3460005D1 (de)
FR (1) FR2540612A1 (de)
IN (1) IN161131B (de)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5535594A (en) * 1993-04-09 1996-07-16 Gaz De France (Service National) Process and apparatus for cooling a fluid especially for liquifying natural gas
US5657643A (en) * 1996-02-28 1997-08-19 The Pritchard Corporation Closed loop single mixed refrigerant process
WO1998057108A1 (en) * 1997-06-12 1998-12-17 Costain Oil, Gas & Process Limited Two-staged refrigeration cycle using a multiconstituant refrigerant
AU701090B2 (en) * 1994-10-05 1999-01-21 Institut Francais Du Petrole Method and installation for the liquefaction of natural gas
US5943881A (en) * 1996-07-12 1999-08-31 Gaz De France (G.D.F.) Service National Cooling process and installation, in particular for the liquefaction of natural gas
US6250244B1 (en) * 1995-10-05 2001-06-26 Bhp Petroleum Pty Ltd Liquefaction apparatus
WO2005017430A1 (de) * 2003-08-14 2005-02-24 Linde Aktiengesellschaft Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes mit gleichzeitiger gewinnung einer c3+-reichen fraktion mit hoher ausbeute
GB2459173A (en) * 2008-04-17 2009-10-21 Linde Ag Method of liquefying a hydrocarbon-rich fraction
CN102575896A (zh) * 2009-04-02 2012-07-11 林德股份公司 液化富烃馏分的方法
JP2016080344A (ja) * 2014-10-10 2016-05-16 エア プロダクツ アンド ケミカルズ インコーポレイテッドＡｉｒ Ｐｒｏｄｕｃｔｓ Ａｎｄ Ｃｈｅｍｉｃａｌｓ Ｉｎｃｏｒｐｏｒａｔｅｄ 天然ガス液化プロセスにおける冷却剤回収
CN105651001A (zh) * 2016-02-25 2016-06-08 上海尧兴投资管理有限公司 适用于不同温度甲烷气的液化系统以及利用该系统液化甲烷气的方法
CN105716369A (zh) * 2010-03-17 2016-06-29 查特股份有限公司 整体式预冷却混合制冷系统和方法
WO2017103533A1 (fr) * 2015-12-17 2017-06-22 Engie Procédé de liquéfaction du gaz naturel a l'aide d'un cycle a mélange réfrigérant avec colonne a distiller du réfrigérant munie d'un rebouilleur
US10480851B2 (en) 2013-03-15 2019-11-19 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
US10663221B2 (en) 2015-07-08 2020-05-26 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
US11408673B2 (en) 2013-03-15 2022-08-09 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
US11428463B2 (en) 2013-03-15 2022-08-30 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method

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US6065305A (en) * 1998-12-30 2000-05-23 Praxair Technology, Inc. Multicomponent refrigerant cooling with internal recycle
FR3016919B1 (fr) * 2014-01-29 2019-04-05 Sun'r Smart Energy Procede de stockage et de restitution d'energie par thermocompression et thermo-detente

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Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5535594A (en) * 1993-04-09 1996-07-16 Gaz De France (Service National) Process and apparatus for cooling a fluid especially for liquifying natural gas
US5613373A (en) * 1993-04-09 1997-03-25 Gaz De France (Service National) Process and apparatus for cooling a fluid especially for liquifying natural gas
AU701090B2 (en) * 1994-10-05 1999-01-21 Institut Francais Du Petrole Method and installation for the liquefaction of natural gas
US6250244B1 (en) * 1995-10-05 2001-06-26 Bhp Petroleum Pty Ltd Liquefaction apparatus
US5657643A (en) * 1996-02-28 1997-08-19 The Pritchard Corporation Closed loop single mixed refrigerant process
US5943881A (en) * 1996-07-12 1999-08-31 Gaz De France (G.D.F.) Service National Cooling process and installation, in particular for the liquefaction of natural gas
WO1998057108A1 (en) * 1997-06-12 1998-12-17 Costain Oil, Gas & Process Limited Two-staged refrigeration cycle using a multiconstituant refrigerant
WO2005017430A1 (de) * 2003-08-14 2005-02-24 Linde Aktiengesellschaft Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes mit gleichzeitiger gewinnung einer c3+-reichen fraktion mit hoher ausbeute
GB2459173A (en) * 2008-04-17 2009-10-21 Linde Ag Method of liquefying a hydrocarbon-rich fraction
GB2459173B (en) * 2008-04-17 2010-11-17 Linde Ag Method of liquefying a hydrocarbon-rich fraction
CN102575896B (zh) * 2009-04-02 2015-04-22 林德股份公司 液化富烃馏分的方法
CN102575896A (zh) * 2009-04-02 2012-07-11 林德股份公司 液化富烃馏分的方法
CN105716369A (zh) * 2010-03-17 2016-06-29 查特股份有限公司 整体式预冷却混合制冷系统和方法
US9441877B2 (en) 2010-03-17 2016-09-13 Chart Inc. Integrated pre-cooled mixed refrigerant system and method
US10502483B2 (en) 2010-03-17 2019-12-10 Chart Energy & Chemicals, Inc. Integrated pre-cooled mixed refrigerant system and method
US10480851B2 (en) 2013-03-15 2019-11-19 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
US11428463B2 (en) 2013-03-15 2022-08-30 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
US11408673B2 (en) 2013-03-15 2022-08-09 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
JP2016080344A (ja) * 2014-10-10 2016-05-16 エア プロダクツ アンド ケミカルズ インコーポレイテッドＡｉｒ Ｐｒｏｄｕｃｔｓ Ａｎｄ Ｃｈｅｍｉｃａｌｓ Ｉｎｃｏｒｐｏｒａｔｅｄ 天然ガス液化プロセスにおける冷却剤回収
US10663221B2 (en) 2015-07-08 2020-05-26 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
EP3954959A2 (de) 2015-07-08 2022-02-16 Chart Energy & Chemicals, Inc. Gemischtes kühlsystem und verfahren
US11408676B2 (en) 2015-07-08 2022-08-09 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
FR3045799A1 (fr) * 2015-12-17 2017-06-23 Engie Procede de liquefaction du gaz naturel a l'aide d'un cycle a melange refrigerant avec colonne a distiller du refrigerant munie d'un rebouilleur
WO2017103533A1 (fr) * 2015-12-17 2017-06-22 Engie Procédé de liquéfaction du gaz naturel a l'aide d'un cycle a mélange réfrigérant avec colonne a distiller du réfrigérant munie d'un rebouilleur
CN105651001B (zh) * 2016-02-25 2018-05-22 上海尧兴投资管理有限公司 适用于不同温度甲烷气的液化系统以及利用该系统液化甲烷气的方法
CN105651001A (zh) * 2016-02-25 2016-06-08 上海尧兴投资管理有限公司 适用于不同温度甲烷气的液化系统以及利用该系统液化甲烷气的方法

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DE3460005D1 (en) 1985-11-07
EP0117793A1 (de) 1984-09-05
CA1227124A (fr) 1987-09-22
FR2540612A1 (fr) 1984-08-10
EP0117793B1 (de) 1985-10-02
AR231586A1 (es) 1984-12-28
IN161131B (de) 1987-10-10
ATE15938T1 (de) 1985-10-15
FR2540612B1 (de) 1985-04-19

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